This specification discloses a reaction device, a reaction method using the reaction
device, and a use of the reaction device. It is an object of the present specification to disclose
a reaction device capable of solving a coking problem that may occur in a process of
15 producing syngas even without applying a method, with high cost and high energy
consumption, of introducing an excessive amount of water vapor or carbon dioxide.
It is an object of the present specification to disclose a reaction device capable of
achieving the above object without using a method with high cost and high energy
consumption even in a DRM process without applying water vapor.
20 It is an object of the present specification to disclose a reaction method using the
reaction device, and a use of the reaction device.
Technical Solution
Among the physical properties mentioned in this specification, the physical property
in which the measurement temperature affects the results is a physical property measured at
25 room temperature, unless otherwise specified.
The room temperature means a natural temperature without warming or cooling. For
example, the room temperature may be any one temperature within a range of 10°C to 30°C,
and may be a temperature of about 23°C or about 25°C or so. The unit of temperature
5
mentioned in this specification is Celsius (°C), unless otherwise specified.
The temperature of the pipeline, internal passage, catalyst section or non-catalyst
section, or the internal temperature of the pipeline, internal passage, catalyst section or noncatalyst section as mentioned in this specification means the center temperature of the
5 pipeline, internal passage, catalyst section or non-catalyst section, unless otherwise specified.
The center temperature is the temperature at the gravity center of the cross section of
the pipeline, internal passage, catalyst section or non-catalyst section. For example, referring
to Fig. 7, the center temperature of the pipeline is indicated as TCenter. Referring to Fig. 7, the
gravity center of the cross section of the pipeline (100) can be confirmed at the specific point
10 (PT) of the pipeline (100), and the temperature TCenter measured at the gravity center can be
referred to as the center temperature at the specific point (PT).
Among the physical properties mentioned in this specification, the physical property
in which the measurement pressure affects the results is a physical property measured at
normal pressure, unless otherwise specified.
15 The term normal pressure means a natural pressure without pressurization and
depressurization. For example, the normal pressure may usually mean about 1 atm or so in a
level of atmospheric pressure.
Unless otherwise specified, the thermodynamic properties mentioned in this
specification are the results measured at 25°C and 1 atm.
20 Among the physical properties mentioned in this specification, the physical property
in which the measurement humidity affects the results is a physical property measured at the
standard-state humidity, unless otherwise specified.
The standard-state humidity is usually a relative humidity, which means a humidity
of about 60% to 65% or so.
25 Among the terms used in this specification, the term “a to b” designating a range
means a range between a and b, including the lower limit of a and the upper limit of b.
This specification discloses a reaction device. The term reaction device means a
device capable of performing any reaction. In one example, the reaction may include an
endothermic reaction. In one example, the reaction may be a reaction in the SMR (Steam
6
Methane Reforming) process, or may be at least some reactions in the SMR (Steam Methane
Reforming) process. In another example, the reaction may be a reaction in the DMR (Dry
Reforming of Methane) process, or may be at least some reactions in the DMR (Dry
Reforming of Methane) process.
5 The reaction device may be a syngas production device, or may be a part of the
syngas production device. Such a syngas production device may be a device in which the
DMR (Dry Reforming of Methane) process is performed in processes.
Hereinafter, the reaction device, and the like will be described with reference to the
drawings according to Examples, but the scope of the reaction device, and the like is not
10 limited to the following.
Fig. 1 is an illustration diagram of an exemplary reaction device (10).
The reaction device (10) may comprise at least one pipeline (100). In the pipeline
(100), an internal passage formed so that a fluid is capable of flowing therethrough may be
included. The shape of the pipeline (100) is not particularly limited, which may be designed
15 by appropriately considering the physical and/or chemical properties, and the like of the fluid
which is a target for the reaction.
Fig. 2 is exemplary shapes of the pipeline (100) of the reaction device (10). The
reaction device (10) in Fig. 1 comprises a pipeline (100) formed in a straight line. Such a
pipeline (100) has a shape that U-shapes are repeatedly equipped, as shown in Fig. 2(a), or is
20 a U-shape, as shown in Fig. 2(b), or may also be in a shape that the shapes, in which Ushaped pipe lines (100) are repeatedly equipped, are arranged to be misaligned so that they do
not overlap each other, as shown in Fig. 2(c).
The cross-sectional shape of the pipeline (100) is not particularly limited. The crosssectional shape of the pipeline (100) may be appropriately designed in consideration of the
25 physical and/or chemical properties of the fluid which is a reaction target. Fig. 3 is exemplary
shapes of cross sections of pipelines (100). The pipeline may have a surface forming the
internal passage. Fig. 3 is shapes of cross sections of pipelines having the surface (110) and
the internal passage (120). As in Fig. 3, the cross section of the pipeline may generally be
circular or quadrangular. In addition to this, the shape of the cross section may be various
30 shapes such as a triangle, diamond, parallelogram, or oval.
A reaction device comprising:
a pipeline having an internal passage configured to allow a fluid to flow through
5 the internal passage;
a catalyst section existing in the internal passage; and
a plurality of heating units,
wherein each of the plurality of heating units is configured to transfer heat energy to
the internal passage independently.
10
[Claim 2]
The reaction device according to claim 1, wherein the catalyst section comprises an
endothermic reaction catalyst.
15 [Claim 3]
The reaction device according to claim 1, wherein a ratio LC/LP of a length LC of the
catalyst section relative to a length LP of the pipeline is 0.3 or more.
[Claim 4]
20 The reaction device according to claim 1, wherein the catalyst section is a continuous
catalyst section.
[Claim 5]
The reaction device according to claim 1, wherein the plurality of heating units
25 comprises an electrical heating unit.
41
[Claim 6]
The reaction device according to claim 5, wherein the electrical heating unit is an
electrical direct heating unit, an electrical indirect heating unit or an induction heating unit.
5 [Claim 7]
The reaction device according to claim 1, wherein the heating units are installed such
that a R1 in the Equation 1 below is in a range from 1 to 100:
[Equation 1]
R1 = LC/HI
10 wherein the LC is a length of the catalyst section, and the HI is an average interval
between the heating units.
[Claim 8]
The reaction device according to claim 1, wherein the heating units are installed such
15 that a R2 in the Equation 2 below is in a range from 0.01 to 10:
[Equation 2]
R2 = LC/n
wherein the LC is a length of the catalyst section and the n is a number of heating units.
20 [Claim 9]
The reaction device according to claim 1, wherein the heating units are installed such
that the catalyst section includes a stabilization section in which a ΔT1 in the Equation 3
below is 2% or less:
[Equation 3]
25 ΔT1 = TS/TCA×100
wherein the TCA is an average temperature of the stabilization section, and the TS is an
42
absolute value of a difference between temperature Ti and the TCA, the temperature Ti being
temperature at any point within the stabilization section.
[Claim 10]
5 The reaction device according to claim 9, wherein the heating units are installed such
that a ratio LS/LC of a length LS of the stabilization section relative to a length LC of the
catalyst section is 0.2 or more.
[Claim 11]
10 The reaction device according to claim 9, wherein the TCA is in a range from 750°C
to 1,000°C.
[Claim 12]
The reaction device according to claim 9, wherein the heating units are installed such
15 that an absolute value of a ΔT2 in the Equation 4 below is in a range from 5% to 60%:
[Equation 4]
ΔT2 = (THA – TCA)/TCA×100
wherein the THA is an average heating temperature of the heating units, and the TCA is
an average temperature of the stabilization section.
20
[Claim 13]
The reaction device according to claim 1, wherein the pipeline further comprises a
non-catalyst section, and the heating units are installed such that the Equation 5 below is
satisfied:
25 [Equation 5]
TNCA ≥ TCL
43
wherein the TNCA is an average temperature of the non-catalyst section, and the TCL is
a lowest temperature of the catalyst section.
[Claim 14]
5 The reaction device according to claim 1, wherein the pipeline further comprises a
non-catalyst section, and the heating units are installed such that Equation 6 below is satisfied:
[Equation 6]
TNCH ≥ TCH
wherein the TNCH is a highest temperature of the non-catalyst section, and the TCH is a
10 highest temperature of the catalyst section.
[Claim 15]
The reaction device according to claim 9, wherein the pipeline further comprises a
non-catalyst section, and an absolute value of a ΔR3 in the Equation 7 below is 20% or less:
15 [Equation 7]
ΔR3 = (TNCA – TCA)/TCA×100
wherein the TCA is an average temperature of the stabilization section, and the TNCA is
an average temperature of the non-catalyst section.
20 [Claim 16]
The reaction device according to claim 9, wherein an absolute value of a ΔR4 in the
Equation 8 below and an absolute value of a ΔR5 in the Equation 9 below are each 20% or
less:
[Equation 8]
25 ΔR4 = (TCH – TCA)/TCA×100
[Equation 9]
44
ΔR5 = (TCL – TCA)/TCA×100
wherein the TCA is an average temperature of the stabilization section, the TCH is a
maximum temperature in the catalyst section, and the TCL is a lowest temperature in the
catalyst section.
5
[Claim 17]
The reaction device according to claim 9, wherein the pipeline further comprises a
non-catalyst section, and an absolute value of a ΔR6 in the Equation 10 below and an absolute
value of a ΔR7 in the Equation 11 below are each 20% or less:
10 [Equation 10]
ΔR6 = (TNCH – TCA)/TCA×100
[Equation 11]
ΔR7 = (TCL – TCA)/TCA×100
wherein, the TCA is an average temperature of the stabilization section, the TNCH is a
15 maximum temperature in the non-catalyst section, and the THCL is a lowest temperature in the
non-catalyst section.
[Claim 18]
The reaction device according to claim 1, wherein the heating units exist at a starting
20 point of the catalyst section, a midpoint of the catalyst section, and an end point of the
catalyst section, respectively, and are installed such that
the Equation 12 below is satisfied,
a ΔT3 in Equation 13 below is a negative number, and its absolute value is in a range
from 1% to 150%, and
25 a ΔT4 in Equation 14 below is a negative number, and its absolute value is in a range
from 0.5% to 150%:
[Equation 12]
45
TCS ≥ TCM ≥ TCE
[Equation 13]
ΔT3 = (TCM – TCS)/TCS×100
[Equation 14]
5 ΔT4 = (TCE – TCM)/TCM×100
wherein, the TCS is an average heating temperature of the heating unit present at the
starting point of the catalyst section, the TCM is an average heating temperature of the heating
unit present at the midpoint of the catalyst section, and the TCE is an average heating
temperature of the heating unit present at the end point of the section.
10
[Claim 19]
The reaction device according to claim 18, further comprising a heating unit at a
point before the catalyst section, wherein it is installed such that
the Equation 15 below is satisfied,
15 a ΔT5 in Equation 16 below is a positive number, and its absolute value is in a range
from 1% to 150%:
[Equation 15]
TCS ≥ TNS
[Equation 16]
20 ΔT5 = (TCS – TNS)/TNS×100
wherein, the TCS is an average heating temperature of the heating unit present at the
starting point of the catalyst section, and the TNS is an average heating temperature of the
heating unit at the point before the catalyst section.
25 [Claim 20]
The reaction device according to claim 18, further comprising a heating unit at a
46
point after the catalyst section,
wherein it is installed such that
the Equation 17 below is satisfied,
a ΔT6 in Equation 18 below is a negative number, and its absolute value is in a range
5 from 0.5% to 50%:
[Equation 17]
TCE ≥ TNE
[Equation 18]
ΔT6 = (TNE – TCE)/TCE×100
10 wherein, the TCE is an average heating temperature of the heating unit present at the
end point of the catalyst section, and the TNE is an average heating temperature of the heating
unit at the point after the catalyst section.
[Claim 21]
15 A method of performing a reaction using the reaction device of claim 1, comprising:
transferring heat energy to the internal passage independently by using two or
more heating units while moving a fluid comprising a reaction target material into the internal
passage of the pipeline.
20 [Claim 22]
The method according to claim 21, wherein the fluid comprises carbon dioxide, does
not comprise water, and comprises an organic hydrocarbon compound.
[Claim 23]
25 The method according to claim 21, wherein the heating units transfer heat energy to
the internal passage such that the catalyst section includes a stabilization section in which a
47
T1 in the Equation 3 below is 2% or less:
[Equation 3]
ΔT1 = TS/TCA×100
wherein the TCA is an average temperature of the stabilization section, and the TS is
5 an absolute value of a difference between temperature Ti and the TCA, the temperature Ti
being temperature at any point within the stabilization section.
[Claim 24]
The method according to claim 23, wherein a ratio LS/LC of a length LS of the
10 stabilization section relative to a length LC of the catalyst section is 0.2 or more.
[Claim 25]
The method according to claim 23, wherein TCA is in a range of 750°C to 1,000°C.
15 [Claim 26]
The method according to claim 23, wherein the heating units transfer heat energy to
the internal passage such that an absolute value of a ΔT2 in the Equation 4 below is in a range
of 5% to 60%:
[Equation 4]
20 ΔT2 = (THA – TCA)/TCA×100
wherein, the THA is an average heating temperature of the heating units, and the TCA
is an average temperature of the stabilization section.
[A reaction device comprising:
a pipeline having an internal passage configured to allow a fluid to flow through
5 the internal passage;
a catalyst section existing in the internal passage; and
a plurality of heating units,
wherein each of the plurality of heating units is configured to transfer heat energy to
the internal passage independently.
10
[Claim 2]
The reaction device according to claim 1, wherein the catalyst section comprises an
endothermic reaction catalyst.
15 [Claim 3]
The reaction device according to claim 1, wherein a ratio LC/LP of a length LC of the
catalyst section relative to a length LP of the pipeline is 0.3 or more.
[Claim 4]
20 The reaction device according to claim 1, wherein the catalyst section is a continuous
catalyst section.
[Claim 5]
The reaction device according to claim 1, wherein the plurality of heating units
25 comprises an electrical heating unit.
41
[Claim 6]
The reaction device according to claim 5, wherein the electrical heating unit is an
electrical direct heating unit, an electrical indirect heating unit or an induction heating unit.
5 [Claim 7]
The reaction device according to claim 1, wherein the heating units are installed such
that a R1 in the Equation 1 below is in a range from 1 to 100:
[Equation 1]
R1 = LC/HI
10 wherein the LC is a length of the catalyst section, and the HI is an average interval
between the heating units.
[Claim 8]
The reaction device according to claim 1, wherein the heating units are installed such
15 that a R2 in the Equation 2 below is in a range from 0.01 to 10:
[Equation 2]
R2 = LC/n
wherein the LC is a length of the catalyst section and the n is a number of heating units.
20 [Claim 9]
The reaction device according to claim 1, wherein the heating units are installed such
that the catalyst section includes a stabilization section in which a ΔT1 in the Equation 3
below is 2% or less:
[Equation 3]
25 ΔT1 = TS/TCA×100
wherein the TCA is an average temperature of the stabilization section, and the TS is an
42
absolute value of a difference between temperature Ti and the TCA, the temperature Ti being
temperature at any point within the stabilization section.
[Claim 10]
5 The reaction device according to claim 9, wherein the heating units are installed such
that a ratio LS/LC of a length LS of the stabilization section relative to a length LC of the
catalyst section is 0.2 or more.
[Claim 11]
10 The reaction device according to claim 9, wherein the TCA is in a range from 750°C
to 1,000°C.
[Claim 12]
The reaction device according to claim 9, wherein the heating units are installed such
15 that an absolute value of a ΔT2 in the Equation 4 below is in a range from 5% to 60%:
[Equation 4]
ΔT2 = (THA – TCA)/TCA×100
wherein the THA is an average heating temperature of the heating units, and the TCA is
an average temperature of the stabilization section.
20
[Claim 13]
The reaction device according to claim 1, wherein the pipeline further comprises a
non-catalyst section, and the heating units are installed such that the Equation 5 below is
satisfied:
25 [Equation 5]
TNCA ≥ TCL
43
wherein the TNCA is an average temperature of the non-catalyst section, and the TCL is
a lowest temperature of the catalyst section.
[Claim 14]
5 The reaction device according to claim 1, wherein the pipeline further comprises a
non-catalyst section, and the heating units are installed such that Equation 6 below is satisfied:
[Equation 6]
TNCH ≥ TCH
wherein the TNCH is a highest temperature of the non-catalyst section, and the TCH is a
10 highest temperature of the catalyst section.
[Claim 15]
The reaction device according to claim 9, wherein the pipeline further comprises a
non-catalyst section, and an absolute value of a ΔR3 in the Equation 7 below is 20% or less:
15 [Equation 7]
ΔR3 = (TNCA – TCA)/TCA×100
wherein the TCA is an average temperature of the stabilization section, and the TNCA is
an average temperature of the non-catalyst section.
20 [Claim 16]
The reaction device according to claim 9, wherein an absolute value of a ΔR4 in the
Equation 8 below and an absolute value of a ΔR5 in the Equation 9 below are each 20% or
less:
[Equation 8]
25 ΔR4 = (TCH – TCA)/TCA×100
[Equation 9]
44
ΔR5 = (TCL – TCA)/TCA×100
wherein the TCA is an average temperature of the stabilization section, the TCH is a
maximum temperature in the catalyst section, and the TCL is a lowest temperature in the
catalyst section.
5
[Claim 17]
The reaction device according to claim 9, wherein the pipeline further comprises a
non-catalyst section, and an absolute value of a ΔR6 in the Equation 10 below and an absolute
value of a ΔR7 in the Equation 11 below are each 20% or less:
10 [Equation 10]
ΔR6 = (TNCH – TCA)/TCA×100
[Equation 11]
ΔR7 = (TCL – TCA)/TCA×100
wherein, the TCA is an average temperature of the stabilization section, the TNCH is a
15 maximum temperature in the non-catalyst section, and the THCL is a lowest temperature in the
non-catalyst section.
[Claim 18]
The reaction device according to claim 1, wherein the heating units exist at a starting
20 point of the catalyst section, a midpoint of the catalyst section, and an end point of the
catalyst section, respectively, and are installed such that
the Equation 12 below is satisfied,
a ΔT3 in Equation 13 below is a negative number, and its absolute value is in a range
from 1% to 150%, and
25 a ΔT4 in Equation 14 below is a negative number, and its absolute value is in a range
from 0.5% to 150%:
[Equation 12]
45
TCS ≥ TCM ≥ TCE
[Equation 13]
ΔT3 = (TCM – TCS)/TCS×100
[Equation 14]
5 ΔT4 = (TCE – TCM)/TCM×100
wherein, the TCS is an average heating temperature of the heating unit present at the
starting point of the catalyst section, the TCM is an average heating temperature of the heating
unit present at the midpoint of the catalyst section, and the TCE is an average heating
temperature of the heating unit present at the end point of the section.
10
[Claim 19]
The reaction device according to claim 18, further comprising a heating unit at a
point before the catalyst section, wherein it is installed such that
the Equation 15 below is satisfied,
15 a ΔT5 in Equation 16 below is a positive number, and its absolute value is in a range
from 1% to 150%:
[Equation 15]
TCS ≥ TNS
[Equation 16]
20 ΔT5 = (TCS – TNS)/TNS×100
wherein, the TCS is an average heating temperature of the heating unit present at the
starting point of the catalyst section, and the TNS is an average heating temperature of the
heating unit at the point before the catalyst section.
25 [Claim 20]
The reaction device according to claim 18, further comprising a heating unit at a
46
point after the catalyst section,
wherein it is installed such that
the Equation 17 below is satisfied,
a ΔT6 in Equation 18 below is a negative number, and its absolute value is in a range
5 from 0.5% to 50%:
[Equation 17]
TCE ≥ TNE
[Equation 18]
ΔT6 = (TNE – TCE)/TCE×100
10 wherein, the TCE is an average heating temperature of the heating unit present at the
end point of the catalyst section, and the TNE is an average heating temperature of the heating
unit at the point after the catalyst section.
[Claim 21]
15 A method of performing a reaction using the reaction device of claim 1, comprising:
transferring heat energy to the internal passage independently by using two or
more heating units while moving a fluid comprising a reaction target material into the internal
passage of the pipeline.
20 [Claim 22]
The method according to claim 21, wherein the fluid comprises carbon dioxide, does
not comprise water, and comprises an organic hydrocarbon compound.
[Claim 23]
25 The method according to claim 21, wherein the heating units transfer heat energy to
the internal passage such that the catalyst section includes a stabilization section in which a
47
T1 in the Equation 3 below is 2% or less:
[Equation 3]
ΔT1 = TS/TCA×100
wherein the TCA is an average temperature of the stabilization section, and the TS is
5 an absolute value of a difference between temperature Ti and the TCA, the temperature Ti
being temperature at any point within the stabilization section.
[Claim 24]
The method according to claim 23, wherein a ratio LS/LC of a length LS of the
10 stabilization section relative to a length LC of the catalyst section is 0.2 or more.
[Claim 25]
The method according to claim 23, wherein TCA is in a range of 750°C to 1,000°C.
15 [Claim 26]
The method according to claim 23, wherein the heating units transfer heat energy to
the internal passage such that an absolute value of a ΔT2 in the Equation 4 below is in a range
of 5% to 60%:
[Equation 4]
20 ΔT2 = (THA – TCA)/TCA×100
wherein, the THA is an average heating temperature of the heating units, and the TCA
is an average temperature of the stabilization section.